US20220153682A1 - Method for producing xylylenediamine - Google Patents

Method for producing xylylenediamine Download PDF

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US20220153682A1
US20220153682A1 US17/438,535 US202017438535A US2022153682A1 US 20220153682 A1 US20220153682 A1 US 20220153682A1 US 202017438535 A US202017438535 A US 202017438535A US 2022153682 A1 US2022153682 A1 US 2022153682A1
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hydrogenation
reaction product
solid
ammonia
liquid separation
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Yukiya Ibi
Tatsuyuki Kumano
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Mitsubishi Gas Chemical Co Inc
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Mitsubishi Gas Chemical Co Inc
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
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    • B01J37/082—Decomposition and pyrolysis
    • B01J37/088—Decomposition of a metal salt
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    • C07C209/00—Preparation of compounds containing amino groups bound to a carbon skeleton
    • C07C209/44—Preparation of compounds containing amino groups bound to a carbon skeleton by reduction of carboxylic acids or esters thereof in presence of ammonia or amines, or by reduction of nitriles, carboxylic acid amides, imines or imino-ethers
    • C07C209/48—Preparation of compounds containing amino groups bound to a carbon skeleton by reduction of carboxylic acids or esters thereof in presence of ammonia or amines, or by reduction of nitriles, carboxylic acid amides, imines or imino-ethers by reduction of nitriles
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/002—Mixed oxides other than spinels, e.g. perovskite
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    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/16—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J23/24—Chromium, molybdenum or tungsten
    • B01J23/28—Molybdenum
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    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/74—Iron group metals
    • B01J23/75—Cobalt
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/74—Iron group metals
    • B01J23/755—Nickel
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J25/00—Catalysts of the Raney type
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
    • B01J27/14—Phosphorus; Compounds thereof
    • B01J27/186—Phosphorus; Compounds thereof with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J27/195—Phosphorus; Compounds thereof with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium with vanadium, niobium or tantalum
    • B01J27/198—Vanadium
    • B01J27/199—Vanadium with chromium, molybdenum, tungsten or polonium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/0009—Use of binding agents; Moulding; Pressing; Powdering; Granulating; Addition of materials ameliorating the mechanical properties of the product catalyst
    • B01J37/0027—Powdering
    • B01J37/0045—Drying a slurry, e.g. spray drying
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C209/00—Preparation of compounds containing amino groups bound to a carbon skeleton
    • C07C209/82—Purification; Separation; Stabilisation; Use of additives
    • C07C209/84—Purification
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C209/00—Preparation of compounds containing amino groups bound to a carbon skeleton
    • C07C209/82—Purification; Separation; Stabilisation; Use of additives
    • C07C209/86—Separation
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C211/00—Compounds containing amino groups bound to a carbon skeleton
    • C07C211/01—Compounds containing amino groups bound to a carbon skeleton having amino groups bound to acyclic carbon atoms
    • C07C211/26—Compounds containing amino groups bound to a carbon skeleton having amino groups bound to acyclic carbon atoms of an unsaturated carbon skeleton containing at least one six-membered aromatic ring
    • C07C211/27—Compounds containing amino groups bound to a carbon skeleton having amino groups bound to acyclic carbon atoms of an unsaturated carbon skeleton containing at least one six-membered aromatic ring having amino groups linked to the six-membered aromatic ring by saturated carbon chains
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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    • B01J2523/00—Constitutive chemical elements of heterogeneous catalysts

Definitions

  • the present invention relates to a method for producing xylylenediamine by hydrogenating dicyanobenzene.
  • Xylylenediamine is a compound useful as a raw material of a polyamide resin, a curing agent, and the like, and an intermediate material of an isocyanate resin and the like.
  • a method for hydrogenating dicyanobenzene has been examined as the method for producing xylylenediamine.
  • Patent Document 1 describes that a nickel-copper-molybdenum-based catalyst is used to catalytically reducing dicyanobenzene, which is brought into contact with hydrogen in liquid phase.
  • Patent Document 2 describes that meta-xylylenediamine can be produced by subjecting isophthalonitrile to batch hydrogenation reaction by an autoclave in the presence of a hydroxide or an alcoholate of an alkali or alkali earth metal and a Raney nickel or Raney Cobalt catalyst in a mixed solvent of a lower alcohol and a cyclic hydrocarbon.
  • Patent Document 3 describes a method for alkali-treating a crude xylylenedi amine
  • Patent Document 4 describes a method for contacting a crude xylylenediamine with a catalyst containing an iron oxide or an oxide of iron and chromium in the presence of water.
  • Patent Document 5 describes that highly pure xylylenediamine can be produced with good yield by hydrogenating dicyanobenzene in two stages in the presence of a solvent.
  • Patent Document 6 describes a production method in which after a first contact hydrogenation reaction of dicyanobenzene is performed using liquid ammonia or a mixed solvent including liquid ammonia and an organic solvent, liquid ammonia is removed to form a reaction product and the resulting reaction product is subjected to a second contact hydrogenation reaction under mild conditions.
  • Patent Document 1 JP S49-133339 A
  • Patent Document 2 JP S54-41804 A
  • Patent Document 3 JP S45-14777 B
  • Patent Document 4 JP S57-27098 B
  • Patent Document 5 JP 2004-292435 A
  • Patent Document 6 JP 2007-332135 A
  • Patent Document 6 The production method described in Patent Document 6 is a useful method for producing highly pure xylylenediamine with a low cyanobenzylamine content.
  • the problem has been found that in this production method, when the reaction is performed for an extended period of time, a differential pressure occurs in the reactor in which the second contact hydrogenation reaction is performed, whereby it is difficult to continuously produce xylylenediamine with a low cyanobenzylamine content. Therefore, from an industrial perspective, there has been a demand for a method that can stably produce a highly pure xylylenediamine over a longer period of time.
  • An object of the present invention is to provide a method that can stably produce a highly pure xylylenediamine with a low cyanobenzylamine content over an extended period of time.
  • an embodiment of the present invention provides a method for producing xylylenediamine, including the following sequential steps:
  • reaction product (A) (1) performing a first hydrogenation including hydrogenating a mixed solution including dicyanobenzene and a solvent containing liquid ammonia in a fixed-bed reactor to form a reaction product (A);
  • Another embodiment of the present invention provides a method for producing xylylenediamine, including the following sequential steps:
  • reaction product (A) (1) performing a first hydrogenation including hydrogenating a mixed solution including dicyanobenzene and a solvent containing liquid ammonia in a fixed-bed reactor to form a reaction product (A);
  • FIG. 1 is a process flow sheet illustrating one aspect of the present invention, that is, steps of hydrogenating dicyanobenzene to produce xylylenediamine.
  • A denotes a first hydrogenation reactor
  • B denotes an ammonia separation distillation column
  • C denotes a solid-liquid separation apparatus
  • D denotes a second hydrogenation reactor.
  • a preferred embodiment (first aspect) of the method for producing xylylenediamine of the present invention includes the following sequential steps:
  • reaction product (A) (1) performing a first hydrogenation including hydrogenating a mixed solution including dicyanobenzene and a solvent containing liquid ammonia in a fixed-bed reactor to form a reaction product (A);
  • Another embodiment (second aspect) of the method for producing xylylenediamine of the present invention includes the following sequential steps:
  • reaction product (A) (1) performing a first hydrogenation including hydrogenating a mixed solution including dicyanobenzene and a solvent containing liquid ammonia in a fixed-bed reactor to form a reaction product (A);
  • the present step is hydrogenating a mixed solution including dicyanobenzene and a solvent containing liquid ammonia in a fixed-bed reactor to form a reaction product (A)
  • Dicyanobenzene used in the present step may be formed by any method, but it is industrially preferable to be formed by ammoxidation reaction of xylene.
  • the ammoxidation reaction can be performed by a known method, and can be performed by feeding and reacting a reaction raw material prepared by mixing a catalyst, xylene, oxygen, and ammonia.
  • the system of the ammoxidation reaction can be either a fluidized bed or a fixed bed.
  • a known catalyst can be used as the catalyst for the ammoxidation, but the catalyst preferably contains vanadium or chromium, and more preferably contains vanadium and chromium.
  • the amount of ammonia is preferably from 2 to 20 mol per one mol of xylene, and more preferably from 6 to 15 mol. When the amount of ammonia is within the range described above, the yield of dicyanobenzene is good, and the space time yield thereof is also high.
  • Oxygen can be also used as an oxygen-containing gas by diluting oxygen with nitrogen, carbon dioxide, or the like. Air is preferably used as the oxygen-containing gas.
  • the amount of oxygen is preferably 3 mol or more and more preferably 4 to 100 mol per one mol of xylene. When the amount of oxygen is within the range described above, the yield of dicyanobenzene is good, and the space time yield thereof is also high.
  • the reaction temperature is preferably 300 to 500° C.
  • Dicyanobenzene formed in the reaction is collected and used as a raw material in the first hydrogenation.
  • a gaseous ammoxidation reaction product may be cooled to a temperature at which dicyanobenzene is deposited and then be collected, or a gaseous ammoxidation reaction product may be collected with water or a suitable organic solvent. It is preferable to collect the ammoxidation reaction product with one or more organic solvents in which solubility of dicyanobenzene is high and which are inert to dicyanobenzene, and it is more preferable to collect dicyanobenzene with tolunitrile.
  • This dicyanobenzene collection solution may be used as is in the first hydrogenation, but it is preferable to separate some or all of components having a lower boiling point than dicyanobenzene including the organic solvent (low-boiling-point components) by distillation before use in the first hydrogenation.
  • the low boiling point components are removed by distillation, and dicyanobenzene is produced.
  • the organic solvent can be used repeatedly in the collection of the reaction product.
  • some or all of components having a higher boiling point than that of dicyanobenzene may be also separated by distillation or extraction.
  • Dicyanobenzene refers to three isomers, phthalonitrile(1,2-dicyanobenzene), isophthalonitrile(1,3-dicyanobenzene), and terephthalonitrile(1,4-dicyanobenzene), and they can be produced from ortho-xylene, meta-xylene, and para-xylene, which are the corresponding xylenes, according to the ammoxidation method.
  • the corresponding xylylenediamines that is, ortho-xylylenediamine, meta-xylylenediamine, and para-xylylenediamine can be formed.
  • the dicyanobenzene in the first hydrogenation is isophthalonitrile
  • the formed xylylenediamine is meta-xylylenediamine.
  • dicyanobenzene is dissolved in a solvent containing liquid ammonia, followed by hydrogenation in the presence of a catalyst in a liquid phase.
  • Examples of the solvent containing liquid ammonia include (i) liquid ammonia, (ii) a mixed solvent of liquid ammonia and an aromatic hydrocarbon, (iii) a mixed solvent of liquid ammonia and xylylenediamine, and (iv) a mixed solvent of liquid ammonia, an aromatic hydrocarbon, and xylylenediamine, and any one selected from these is preferable.
  • One aromatic hydrocarbon may be used and two or more aromatic hydrocarbons may be used in combination.
  • the concentration of liquid ammonia in the solvent is preferably higher and specifically, it is more preferably 60 mass % or higher and further preferably 100 mass %.
  • the amount of the solvent containing liquid ammonia in the present step is preferably 1 to 99 parts by mass, more preferably 3 to 66 parts by mass, and further preferably 5 to 49 parts by mass, per 1 part by mass of dicyanobenzene.
  • amount of the solvent is within the range described above, energy required for solvent recovery is low, which is economically advantageous, and the selection rate of xylylenediamine in the hydrogenation reaction is also favorable.
  • Dicyanobenzene may be dissolved in a solvent containing liquid ammonia by using a mixer such as a static mixer, but from the perspective of preventing a deposited insoluble matter from adhering to the mixer or the like, it is preferable to dissolve dicyanobenzene by mixing dicyanobenzene and the solvent in advance in a dissolution tank. It is more preferable to dissolve dicyanobenzene by feeding molten dicyanobenzene and the solvent into the dissolution tank, and stirring may be performed as necessary.
  • the pressure and temperature in the dissolution tank are preferably adjusted such that the solution remains in the liquid phase.
  • the pressure in the dissolution tank is preferably from 0.5 to 15 MPa, more preferably from 0.7 to 10 MPa, and further preferably from 1 to 8 MPa.
  • the solution temperature in the dissolution tank is preferably 3 to 140° C., more preferably 5 to 120° C., and further preferably 10 to 100° C.
  • the insoluble component may be removed by solid-liquid separation before feeding the solution to the hydrogenation reactor.
  • solid-liquid separation a known method such as filtration, centrifugation, and sedimentation can be used, but filtration is preferable, and filtration by a sintered metal filter and/or strainer is particularly convenient and suitable.
  • the system of the hydrogenation reaction in the present step is a fixed bed, and the hydrogenation reaction is performed using a fixed-bed reactor.
  • the fixed-bed reaction may be of a batch type or a continuous type, but a continuous type is preferable in order to sufficiently exert the effects of the present invention.
  • a circulating system When continuous reaction is performed, a circulating system may be used in which some of the hydrogenation reaction solution formed from an outlet of the hydrogenation reactor is continuously returned to the hydrogenation reactor, or a combination of a circulating system and a one-pass system may be used as described in JP 2008-31155 A.
  • the hydrogenation reaction time is preferably from 0.5 to 8 hours.
  • catalyst used in the fixed-bed reactor in the present step known supported metal catalysts, unsupported metal catalysts, Raney catalysts, sponge catalysts, noble metal catalysts, and the like can be used. Particularly, it is preferable to use a catalyst containing nickel and/or cobalt.
  • the amount of catalyst used may be an amount used for the known liquid phase hydrogenation of dicyanobenzene.
  • Hydrogen used in the present step may include impurities such as methane and nitrogen that do not participate in the reaction, but when the impurity concentration is high, the total pressure of the reaction needs to be increased in order to ensure the required hydrogen partial pressure, which is industrially disadvantageous.
  • the hydrogen concentration is preferably 50 mol % or greater, and more preferably 80 mol % or greater.
  • the present step in order to efficiently produce xylylenediamine, it is essential to increase the degree of progression of the hydrogenation reaction of a nitrile group to an aminomethyl group, and it is preferable to select a reaction condition such that the concentrations of dicyanobenzene and cyanobenzylamine in the liquid formed after the hydrogenation reaction are kept low.
  • the amount of cyanobenzylamine relative to xylylenediamine in the solution after the hydrogenation reaction (reaction product (A)) is preferably maintained at 5.0 mass % or less, more preferably 1.0 mass % or less, and further preferably 0.2 mass % or less.
  • the conversion rate of dicyanobenzene is preferably 99.50% or greater, and more preferably 99.90% or greater, and further preferably 99.95% or greater.
  • the pressure and temperature of the hydrogenation reaction are preferably adjusted so that the solution remains in the liquid phase.
  • the temperature of the hydrogenation reaction is preferably 20 to 200° C., more preferably 30 to 150° C., and further preferably 40 to 120° C.
  • the hydrogen pressure is preferably 1 to 30 MPa, more preferably 2 to 25 MPa, and further preferably 3 to 20 MPa.
  • the present step is ammonia separation in which the liquid ammonia included in the reaction product (A) is separated and removed to form a reaction product (B).
  • the present step includes separating and removing all or part of the liquid ammonia in the solvent including liquid ammonia used in the previous step.
  • a solvent other than liquid ammonia such as an aromatic hydrocarbon
  • only the liquid ammonia may be separated and removed, and the liquid ammonia and the solvent other than liquid ammonia may be simultaneously separated and removed, but from an industrial perspective, it is preferable to simultaneously separate and remove the liquid ammonia and the solvent other than the liquid ammonia.
  • the method for separating and removing liquid ammonia is not limited, but separation and removal by distillation is preferable.
  • the distillation is preferably performed under pressurized conditions, and the pressure is preferably from 0.2 to 3 MPa.
  • the temperature is preferably 50 to 200° C., and more preferably 70 to 180° C.
  • distillation apparatus used in the present step, a known distillation apparatus such as a packed column, a shelf column, and a flash drum can be used, and distillation is performed in batches or continuously.
  • the amount of ammonia in the solution containing xylylenediamine formed after distillation of the present step is preferably 1.0 mass % or less.
  • the amount of ammonia is 1.0 mass % or less, it is possible to prevent an increase in the partial pressure of the solution after distillation, and thus a high-pressure reactor is unnecessary in a subsequent process, which is economically advantageous.
  • the present step is solid-liquid separation including subjecting the reaction product (B) to solid-liquid separation and removing a solid component to form a reaction product (C).
  • the solid component in the present step is an insoluble matter generated in the step described above, but the main component is considered to be catalyst powder derived from a catalyst used in a fixed-bed reactor, specifically, the main component is considered to be catalyst fine powder having a particle size of 1 to 500 ⁇ m.
  • a known method may be used for the solid-liquid separation, but is preferably adsorption, filtration, or sedimentation, more preferably adsorption or filtration, and further preferably adsorption.
  • Examples of the adsorption include magnetic adsorption and adsorption by intermolecular forces, and magnetic adsorption is preferable.
  • the use of magnetic adsorption can efficiently remove catalyst fine powder derived from a catalyst having a component including ferromagnetic properties such as nickel and cobalt used in the first hydrogenation, whereby a solution (reaction product (C)) in which little amount of catalyst fine powder remains can be obtained.
  • the magnetic adsorption is preferably adsorption using a magnet filter.
  • the magnetic force of the magnet filter is desirably set to be capable of removing the catalyst fine powder, while the size of the magnet filter, the flow rate of the solution, and the like are taken into consideration.
  • the magnetic force is preferably from 0.1 to 3 tesla (T) and more preferably from 0.5 to 2 tesla (T).
  • the filter used for the filtration is not particularly limited, but filtration using a sintered metal filter is preferable.
  • the filter size of the sintered metal filter is preferably 100 ⁇ m or less, and more preferably 50 ⁇ m or less, and further preferably 10 ⁇ m or less.
  • the sintered metal filter having the filer size of 100 ⁇ m or less can efficiently remove the catalyst fine powder flowing out from the first hydrogenation step.
  • sedimentation examples include static separation and centrifugal separation.
  • the present step is a second hydrogenation including hydrogenating the reaction product (C) in a fixed-bed reactor.
  • the hydrogenation in the present step is preferably performed in a continuous fixed-bed reaction.
  • the catalyst used in the present step known supported metal catalysts, unsupported metal catalysts, Raney catalysts, sponge catalysts, noble metal catalysts, and the like can be used. Particularly, catalysts containing nickel and/or cobalt are suitably used.
  • the solvent other than liquid ammonia may be left unremoved in the ammonia separation and used as is in the present step. That is, the reaction product (B) formed in the ammonia separation step (2) may contain a solvent, and the reaction product containing a solvent formed after (3) the solid-liquid separation step may be used as the reaction product (C) in the present step.
  • the temperature of the hydrogenation reaction is preferably 30 to 150° C., more preferably 40 to 120° C., and further preferably 50 to 100° C.
  • the hydrogen pressure of the hydrogenation reaction is preferably from 0.1 to 10 MPa, more preferably from 0.5 to 8 MPa, and further preferably from 1 to 4 MPa.
  • the space velocity (LHSV) of the reaction raw material is preferably from 0.1 to 10 h ⁇ 1 , and more preferably from 0.1 to 3.0 h ⁇ 1 .
  • the space velocity is 0.1 h ⁇ 1 or greater, the amount that can be handled per unit time increases, which is industrially advantageous.
  • the space velocity is 10 h ⁇ 1 or less, the conversion rate of cyanobenzylamine can be increased.
  • the hydrogenation reaction time is preferably from 0.5 to 8 hours.
  • the amount of cyanobenzylamine relative to xylylenediamine in the solution formed after the hydrogenation reaction is preferably maintained at 0.02 mass % or less, more preferably 0.01 mass % or less, further preferably 0.005 mass % or less, and even further preferably 0.001 mass % or less.
  • the reaction conditions such as temperature, hydrogen pressure, reaction time, or LHSV so as to maintain an amount of cyanobenzylamine in the aforementioned range, highly pure xylylenediamine can be formed.
  • the present step is purifying xylylenediamine after the second hydrogenation (4).
  • the method preferably includes the purification (5) from the perspective of purifying the reaction product formed in the second hydrogenation (4) to form a more highly pure xylylenediamine.
  • the purification method in the present step is preferably a method by distillation, and it is preferable to use a distillation column having a theoretical number of stages of 2 or more, and more preferably a distillation column having a theoretical number of stages of 5 or more.
  • distillation is preferably performed under a reduced pressure, and the pressure is preferably from 1 to 10 kPa.
  • a second aspect of the method for producing xylylenediamine is a method in which the ammonia separation (2) and the solid-liquid separation (3) of the above method for producing xylylenediamine are reversed.
  • it is a method for producing xylylenediamine including the following sequential steps:
  • reaction product (A) (1) a first hydrogenation including hydrogenating a mixed solution including dicyanobenzene and a solvent containing liquid ammonia in a fixed-bed reactor to form a reaction product (A);
  • a method for producing xylylenediamine including the two processes for producing xylylenediamine includes the following steps:
  • reaction product (A) (1) a first hydrogenation including hydrogenating a mixed solution including dicyanobenzene and a solvent containing liquid ammonia in a fixed-bed reactor to form a reaction product (A);
  • step (1) in which after step (1), step (2) and step (3) are performed in this order or reverse order, followed by step (4).
  • step (3) is performed before step (2)
  • the reaction product (A) is subjected to solid-liquid separation in step (3) to form the reaction product (D)
  • the liquid ammonia included in the reaction product (D) is separated and removed in step (2) to form the reaction product (E)
  • step (2) is performed before step (3)
  • the liquid ammonia included in the reaction product (A) is separated and removed in step (2) to form the reaction product (B)
  • the reaction product (B) is subjected to solid-liquid separation in step (3) to form the reaction product (C).
  • the method for producing xylylenediamine according to an embodiment of the present invention is a method including the following sequential steps:
  • reaction product (A) (1) a first hydrogenation including hydrogenating a mixed solution including dicyanobenzene and a solvent containing liquid ammonia in a fixed-bed reactor to form a reaction product (A);
  • a first hydrogenation including hydrogenating a mixture including dicyanobenzene and a solvent containing liquid ammonia in a fixed-bed reactor to form a reaction product (A);
  • each production condition is preferably that described above, and after step (4), the purification (5) is more preferably performed.
  • the reaction product (B) in step (3) is substituted with the reaction product (A)
  • the reaction product (C) is substituted with the reaction product (D)
  • the reaction product (A) in step (2) is substituted with the reaction product (D)
  • the reaction product (B) is substituted with the reaction product (E).
  • Isophthalonitrile used in the Examples was synthesized as follows.
  • vanadium pentoxide available from FUJIFILM Wako Pure Chemical Corporation, guaranteed
  • 500 mL of water distilled water
  • 477 g of oxalic acid available from FUJIFILM Wako Pure Chemical Corporation, guaranteed
  • This catalyst solution was spray-dried while maintaining an inlet temperature of 250° C. and an outlet temperature of 130° C. After drying for 12 hours in a dryer at 130° C., the product was baked for 0.5 hours at 400° C., and then baked at 550° C. for 8 hours under air flow.
  • the catalyst had an atomic ratio of V:Cr:B:Mo:P:Na:K of 1:1:0.5:0.086:0.007:0.009:0.020, and the catalyst concentration was 50 mass %.
  • An ammoxidation reactor is charged with 6 L of the flow catalyst prepared above, and air, meta-xylene (hereinafter, abbreviated as MX, available from Mitsubishi Gas Chemical Company) and ammonia (available from Mitsubishi Gas Chemical Company) were mixed, then preheated to 350° C. and fed to the reactor.
  • MX meta-xylene
  • ammonia available from Mitsubishi Gas Chemical Company
  • the preparation conditions were set such that the MX feed rate was 350 g/h, the molar ratio of ammonia/MX was 11, the molar ratio of oxygen/MX was 5.4, and the space velocity GHSV was 630 h ⁇ 1 .
  • the reaction temperature was set to 420° C. and the reaction pressure was set to 0.2 MPa.
  • the gaseous reaction product from the top of the ammoxidation reactor was introduced into an isophthalonitrile absorption column, and isophthalonitrile in the reaction product was absorbed and collected in meta-tolunitrile (available from Mitsubishi Gas Chemical Company).
  • the isophthalonitrile absorption column was made of SUS304, and had a condenser on the upper part thereof, a body part having an inner diameter of 100 mm ⁇ and a height of 800 mm, a lower part of the body part, which was 450 mm in length, having a structure of a double pipe for allowing steam-heating, and a gas blow inlet being provided at the bottom.
  • the above absorption liquid was fed to the middle stage of a distillation column for low boiling point component separation.
  • a column top pressure was set to 6 kPa
  • a column top temperature was set to 120° C.
  • a column bottom temperature was set to 183° C.
  • a residence time at the column bottom was set to 60 minutes.
  • the meta-tolunitrile and other low-boiling point components were distilled off at the column top of the distillation column, and isophthalonitrile was extracted from the column bottom.
  • the purity of the produced isophthalonitrile was 96.4 mass %.
  • the resulting isophthalonitrile was used in the following Examples.
  • a tubular vertical hydrogenation reactor (in FIG. 1 , first hydrogenation reactor A) (made of SUS304, inner diameter of 150 mm ⁇ ) was filled with 18 kg of a commercially available supported nickel/diatomaceous earth catalyst (cylindrical shape, diameter of 5 mm ⁇ , height of 5 mm) having a nickel content of 50 mass % and the catalyst was reduced at 200° C. under hydrogen gas flow to be activated. After cooling, hydrogen gas was introduced into the reactor under pressure, held at a constant pressure of 8 MPa, and the catalyst layer temperature was maintained at 100° C. by heating externally.
  • the amount of reaction intermediate 3-cyanobenzylamine produced increased over time, and the reaction was ended when the amount of 3-cyanobenzylamine relative to meta-xylylenediamine contained in the hydrogenation reaction solution reached 0.2 mass %.
  • the reaction solution after the first hydrogenation was fed to an ammonia separation distillation column (in FIG. 1 , ammonia separation distillation column B), ammonia was distilled and separated at a column bottom temperature of 150° C. and 0.5 MPa, and liquid ammonia was recovered from the column top.
  • the composition of the reaction solution produced from the column bottom was 91.4 mass % meta-xylylenediamine and 0.18 mass % 3-cyanobenzylamine, and no isophthalonitrile was detected.
  • fine powder of the catalyst used in the first hydrogenation step was found in the produced reaction solution.
  • a tubular vertical hydrogenation reactor (in FIG. 1 , second hydrogenation reactor D) (made of SUS304, inner diameter of 30 mm ⁇ ) was filled with 150 g of a commercially available supported nickel/diatomaceous earth catalyst (cylindrical shape, diameter of 3 mm ⁇ , height of 3 mm) having a nickel content of 50 mass %, and the catalyst was reduced at 200° C. under hydrogen gas flow to be activated.
  • hydrogen gas was introduced into the reactor under pressure, held at a constant pressure of 2 MPa, and the catalyst layer temperature was maintained at 80° C. by heating externally. Thereafter, while circulating hydrogen gas from the upper portion of the reactor at a flow rate of 3 NL/h, the reaction solution after the solid-liquid separation was continuously fed at a rate of 75 g/h.
  • Increase of the differential pressure between the top and bottom of the catalyst layer was 10 kPa or less even after 300 days from the start of the reaction.
  • the composition of the reaction solution formed after 300 days from the start of the reaction was 91.0 mass % of meta-xylylenediamine and 0.001 mass % or less of 3-cyanobenzylamine.
  • the reaction solution after the second hydrogenation was distilled using a distillation column with a theoretical number of 10 stages under a reduced pressure of 6 kPa to produce meta-xylylenediamine purified to a purity of 99.99%.
  • the 3-cyanobenzylamine content in the produced meta-xylylenediamine was 0.001 mass % or less.
  • the first hydrogenation was performed in the same manner as in Example 1 except that 18 kg of the supported nickel/diatomaceous earth catalyst, which was a hydrogenation catalyst, was changed to 28.8 kg of a commercially available Raney cobalt catalyst having a cobalt content of 50 mass %, and the reaction was ended at a time when the amount of 3-cyanobenzylamine relative to meta-xylylenediamine in the hydrogenation reaction solution reached 0.2 mass %.
  • reaction solution after the first hydrogenation was fed to an ammonia separation distillation column, and ammonia was distilled and separated at a column bottom temperature of 150° C. and 0.5 MPa, and liquid ammonia was recovered from the column top.
  • composition of the reaction solution produced from the column bottom was 92.8 mass % meta-xylylenediamine and 0.18 mass % 3-cyanobenzylamine, and no isophthalonitrile was detected.
  • fine powder of the catalyst used in the first hydrogenation was found in the produced reaction solution.
  • the second hydrogenation step was performed in the same manner as in Example 1. Increase of the differential pressure between the top and bottom of the catalyst layer was 10 kPa or less even after 300 days from the start of the reaction.
  • the composition of the reaction solution produced after 300 days from the start of the reaction was 92.4 mass % of meta-xylylenediamine and 0.001 mass % or less of 3-cyanobenzylamine.
  • the reaction solution after the second hydrogenation was distilled using a distillation column with a theoretical number of 10 stages under a reduced pressure of 6 kPa to produce a meta-xylylenediamine purified to a purity of 99.99%.
  • the 3-cyanobenzylamine content in the produced meta-xylylenediamine was 0.001 mass % or less.
  • the steps up to the second hydrogenation were performed in the same manner as in Example 1 except that the step of (3) solid-liquid separation was excluded.
  • the differential pressure between the top and bottom of the catalyst layer gradually increased in the second hydrogenation reactor, the differential pressure reached 300 kPa at the time when 255 days elapsed after the start of the reaction (accumulated fed amount of the reaction solution of 459 kg), and it became impossible to maintain the amount of 3-cyanobenzylamine in the meta-xylylenediamine at 0.001 mass % or less.
  • the composition of the reaction solution produced after 255 days from the start of the reaction was 90.9 mass % of meta-xylylenediamine and 0.011 mass % of 3-cyanobenzylamine.

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